Increasing thermal dissipation of fuel cell stacks under partial electrical load

ABSTRACT

A method of operating a high temperature fuel cell system containing a plurality of fuel cell stacks includes operating one or more of the plurality of fuel cell stacks at a first output power while operating another one or more of the plurality of the fuel cell stacks at a second output power different from the first output power.

This application is a Divisional of U.S. application Ser. No.12/591,872, filed Dec. 3, 2009, which is a Divisional of U.S.application Ser. No. 11/125,267, filed May 10, 2005, now U.S. Pat. No.7,700,210, which are incorporated herein by reference in their entirety.

BACKGROUND OF THE INVENTION

The present invention is generally directed to fuel cells and morespecifically to fuel cell systems and their operation.

Fuel cells are electrochemical devices which can convert energy storedin fuels to electrical energy with high efficiencies. High temperaturefuel cells include solid oxide and molten carbonate fuel cells. Thesefuel cells may operate using hydrogen and/or hydrocarbon fuels. Thereare classes of fuel cells, such as the solid oxide regenerative fuelcells, that also allow reversed operation, such that oxidized fuel canbe reduced back to unoxidized fuel using electrical energy as an input.

In a high temperature fuel cell system such as a solid oxide fuel cell(SOFC) system, an oxidizing flow is passed through the cathode side ofthe fuel cell while a fuel flow is passed through the anode side of thefuel cell. The oxidizing flow is typically air, while the fuel flow istypically a hydrogen-rich gas created by reforming a hydrocarbon fuelsource. The fuel cell, operating at a typical temperature between 750°C. and 950° C., enables the transport of negatively charged oxygen ionsfrom the cathode flow stream to the anode flow stream, where oxygen fromoxygen ions combines with either free hydrogen or hydrogen in ahydrocarbon molecule to form water vapor and/or with carbon monoxide toform carbon dioxide. The excess electrons from the negatively chargedion are routed back to the cathode side of the fuel cell through anelectrical circuit completed between anode and cathode, resulting in anelectrical current flow through the circuit.

In most applications of high temperature fuel cells, a number of cellsare connected in series forming a cell “stack.” Cells connected inseries operate at the same current and are thereby locked to the sameoperating state. In order to operate efficiently, these fuel cells inthe stack have to be maintained at or near their nominal or designedoperating temperature. The fuel cells are usually designed to operate ata high or even a maximum load at which the fuel cells achieve thenominal or designed operating temperature. Thus, under high electricalloads, high temperature fuel cell stacks dissipate enough heat tomaintain their nominal or designed operating temperature (providedadequate thermal management/insulation). However, sometimes the fuelcells operate at a partial or low load, which is lower than the designedhigh or maximum operating load. This may occur when there is low powerdemand on the fuel cell stack, for example. At partial or low load, theamount of heat dissipated quickly tapers off and the high temperaturefuel cell stack may drop in operating temperature. Generally, a drop inoperating temperature may be acceptable, but at lower temperature thestack has reduced power generation capabilities and may be unable toprovide sufficient power when the power demand increases suddenly.

BRIEF SUMMARY OF THE INVENTION

One aspect of present invention provides a method of operating a hightemperature fuel cell system containing a plurality of fuel cell stacks.The method comprises operating one or more of the plurality of fuel cellstacks at a first output power while operating another one or more ofthe plurality of the fuel cell stacks at a second output power differentfrom the first output power.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a plot of voltage, electrical power density, and heatdissipated versus current for a fuel cell.

FIG. 2 is a plot of electrical power density versus heat dissipated.

FIGS. 3A and 3B are schematic side cross sectional views of systems ofthe embodiments of the present invention.

FIGS. 4A and 5A are top cross sectional views of portions of the systemof FIG. 3B.

FIGS. 4B and 5B are side cross sectional views of portions of the systemof FIG. 3B which correspond to the portions shown in FIGS. 4A and 5A,respectively.

FIG. 6A is a top cross sectional view of a portion of the system of FIG.3A.

FIG. 6B is a side cross sectional view of a portion of the system ofFIG. 3A, which corresponds to the portion shown in FIG. 6A.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

In one embodiment of the invention, the present inventors realized thatin a fuel cell system containing a plurality of fuel cell stacks, if theone or more stacks in the system are operating at a lower output powerthan one or more other stacks, while the sum of the output power fromall of the stacks in the system still meets the total required ordesired output power, then the combined thermal dissipation of thestacks will be higher compared to operation of all the stacks in thesystem at equal output power. Thus, operating different stacks atdifferent output power from each other while the sum of the output powerfrom the stacks in the system still meets the total required or desiredoutput power provides a higher heat dissipation. Each stack is thermallyintegrated with one or more other stacks, such that each stack providesdissipated heat to one or more other stacks and/or absorbs heat from oneor more other stacks. The stacks may be operated at different outputpower during partial or low system load to increase the heatdissipation. Alternatively, the stacks may be operated at differentoutput power during high or maximum system load to increase the heatdissipation if the heat dissipation during high or maximum load is notsufficient when the stacks all operate at the same output power. Itshould be noted that the term “output power” as used herein generallyrefers to the output power density measured in the units of Watts perunit area of the fuel cells in the stack.

FIG. 1 shows the voltage, electrical power density (per unit area), andheat dissipation density (per unit area) by a single, typical SOFC as afunction of current density (per unit area). The voltage can beadequately described as a linear function of current density (with theslope being the “area specific resistance” (“ASR”)). Power, which iscurrent times voltage, is therefore a quadratic function of current.Heat dissipation of a cell is also a quadratic function of current. FIG.2 shows the same data as FIG. 1 with the heat dissipation densityplotted against electrical (i.e., output) power density. It can be seenthat dissipation density increases in a square root fashion rather thanin a linear function when output power density approaches its maximum.This indicates that a reduction in output power density will lead to alargely over proportional reduction in heat dissipation density, whichat low output power density creates difficulties for maintaining celloperating temperature.

In a fuel cell system containing a plurality of stacks, the stacks canbe separately connected to the power system containing at least one of apower conditioning subsystem and a power control subsystem, and therebyindividually controlled, with different stacks providing differentoutput power. Individual stack control allows an increase in heatdissipation at low or partial electrical load.

In one non-limiting example of the above principle, the system containstwo stacks. If one stack is operated above half of the total desired orrequired output power and the other stack is operated below half of thetotal desired or required output power, such that the sum of the outputpower still meets the total desired or required output power, then thecombined thermal dissipation of the two stacks will be higher comparedto operation of both stacks at an equal output power of half the totaldesired or required output power.

For example, if the total desired output power of the system equals 0.4W/cm², and if the first stack is operated at 0.25 W/cm², and the secondstack is operated at 0.15 W/cm², then the total system output powerwould equal to 0.4 W/cm², and the total system heat dissipation wouldequal to about 0.15 W/cm² from FIG. 2 (i.e., 0.12 W/cm² from the firststack +0.03 W/cm² from the second stack). In contrast, if both stacksare operated at 0.2 W/cm², then the total system output power wouldstill equal to 0.4 W/cm², but the total system heat dissipation wouldequal to only about 0.12 W/cm² from FIG. 2 (i.e., 0.06 W/cm² from boththe first and the second stacks). Thereby, the nonlinear relationshipbetween power and heat dissipation shown in FIG. 2 is advantageouslyused to increase the total system heat dissipation without changing thesystem output power. In the two stack system example described above, anabout 20% increase in heat dissipation may be obtained by varying theoutput power of each stack by 0.05 W/cm² from the 50% value of the totaldesired output power. This simple scheme allows system operation atreduced loads while maintaining reasonably high thermal dissipation.

It should be noted that the above described method is not limited tooperating two stacks at different output power. For example, the systemmay contain three or more stacks, such as four to ten stacks forexample. The stacks in the system may be separated into two or morearbitrary sets of stacks, where each set contains one or more stacks.Stacks in different sets operate at different output powers, but stacksin the same set operate at the same power. Thus, the stacks in thesystem may be operating at the same time at three or more differentoutput powers if desired.

In one aspect of the invention, a software program is used to determinethe optimum distribution of output powers of the stacks in the system.In this case, the corresponding heat dissipation data for each outputpower of each stack (i.e., data similar to that shown in FIG. 2) isprovided into the software along with the number of stacks in thesystem, the desired or required total output power of the system, andany other parameters, such as the number of sets of stacks which operateat different output powers (i.e., the number of different output powersprovided from the stacks). The program then solves an optimizationequation to determine the preferred output power for stack to obtain thedesired or required heat dissipation.

In a first embodiment of the invention, separate power conversionequipment connection and preferably separate fuel supplies are providedfor every stack in order to increase the thermal dissipation byoperating different stacks at different output power. In thisembodiment, as shown in FIGS. 3A and 3B, a separate fuel inlet conduitand a separate fuel flow control device is provided for each stack. Theamount of fuel being provided into each stack is controlled incoordination with the output power of the stacks. Thus, less fuel isprovided into the stacks that are operating at lower output power thaninto the stacks that are operating at higher output power to avoidwasting fuel. In other words, the amount of fuel provided to each of theplurality of fuel cell stacks is preferably but not necessarilyseparately controlled, such that more fuel is provided to one or morestacks operating at the first output power than to one or more stacksoperating at the second output power which is lower than the firstoutput power. Each stack is separately electrically connected to thepower system which contains one or both of a conditioningsubsystem/power controller. For example, a separate inverter dedicatedto each stack or each set of stacks may be provided. It should be notedthat if two or more stacks are grouped into a set of stacks that areadapted to operate at the same output power, then such stacks may sharea common fuel inlet conduit and/or be connected in series to the powersystem.

In a second embodiment of the invention, the increased thermaldissipation is obtained without utilizing separate fuel feed conduitsand controllers for each stack. In the method of the second embodiment,a difference in time response between the electrical and the fuel (i.e.,gas) subsystems is exploited. In the second embodiment, the load on thestacks is varied at a rate much faster than time constants involved inthe (local) fuel transport to multiple stacks. Thus, multiple fuel cellstacks can operate at different output power levels on a common fuelsupply while subject to load changes. In this embodiment, the change incurrent occurs fast enough to avoid local fuel or oxidizer starvation ofthe cells in the stack. This may require load variations in the kHzregime or higher. Thus, the output power of the stacks in varied fasterthan the time it takes for local fuel or oxidizer starvation of thecells in the stack to set in.

For example, in case of two stacks, the first stack is operated at ahigher output power and the second stack is operated at a lower powerfor a short period of time (i.e., for a period of time shorter than thetime it takes for local fuel or oxidizer starvation of the cells in thestack to set in). Then, the output power of the stacks is switched, suchthat the first stack is operated at a lower power and the second stackis operated at a higher power for a short period of time (i.e., for aperiod of time shorter than the time it takes for local fuel or oxidizerstarvation of the cells in the stack to set in). Then, the output powerof the stacks is changed again such that the first stack is againoperated at a higher output power and the second stack is again operatedat a lower power for a short period of time. Thus, the load on thestacks is switched or alternated frequently, for example, at least onceevery one thousandths of a second (i.e., with a load variation frequencyof 1 kHz or higher) to avoid local fuel or oxidizer starvation of thecells. It should be noted that more than two stacks and/or more than twooutput powers may be used, as described above. In this case a pluralityof fuel cell stacks comprise at least a first set of fuel cell stackscontaining one or more first stacks and a second set of fuel cell stackscontaining one or more second stacks. Preferably, the same amount offuel is provided to each of the one or more first fuel cell stacks andto each of the one or more second fuel cell stacks. The load on thefirst and the second sets of stacks is repeatedly varied such that theoutput power of the first is alternately higher or lower than the outputpower of second sets of stacks. The output power/load switching ispreferably conducted by an automated controller, such as a computer orlogic circuit. Furthermore, software or hardware may be used todetermine an optimum switching frequency and output power for thesystem.

It is believed that heat dissipation is mostly ohmic and will respondinstantaneously to changes in stack load/output power. However, thethermal response of the system is typically slower than the fluidssystem. Therefore, this load modulation will cause negligibletemperature oscillations of the system as a whole. The relationshipbetween the time constants of the mechanisms in the system of the secondembodiment is illustrated in equation 1:τ_(electrical)<<τ_(fluid)  (1)

If multiple stacks are independently connected to a power system (i.e.,to a single power conditioning subsystem/controller that is able toindependently control the stack load and output power, or to a pluralityof independent power conditioning subsystems/controllers each of whichis associated with one or more stacks of the system), then these loadmodulations can be executed with a constant net stack output. Forexample, a separate inverter dedicated to each stack or each set ofstacks may be provided.

If a multitude of stacks is simultaneously load modulated, the netoutput of the stacks may fluctuate. For a load modulation at highfrequency, the energy storage required to level the stack output issmall and can easily be provided by one or more capacitors or batterieswhich may already be a part of the system. Thus, one or more capacitorsand/or batteries can be used to store excess energy generated duringoutput power spikes and then release the stored energy during outputpower dips to provide a substantially even power output from the system.

It should be noted that the stack load modulations may include reversedcurrent operation of one or more stacks (i.e., reversing a polarity ofcurrent provided to the stacks). Thus, rather than decreasing the poweroutput of some stacks, the stacks may be temporarily operated in theso-called electrolysis mode, where the stacks draw electrical energyfrom the power conditioning system rather than provide electrical energyto the power conditioning system. These temporary current inversions onfuel cells may reduce cell degradation and thereby increase performance.Without wishing to be bound by a particular theory, it is believed thatif a suitable reducing or inert atmosphere is provided to the fuel cellfuel (i.e., anode) electrodes, then the cermet in the fuel electrodesmay be reduced during the current inversions to improve the operation ofthe fuel cells. Examples of the fuel electrode cermets include nickeland yttria stabilized zirconia containing cermets and examples of areducing or inert atmosphere include nitrogen, hydrogen or argon.

In a third embodiment of the invention, an output power of one or morestacks is periodically cycled (i.e., varied) above and below an averagedesired or required output power, such that the output powersubstantially equals the average desired or required output power over aperiod of time. In this embodiment, the fuel cell stacks need not bethermally integrated with other stacks (i.e., the fuel cell stacks maybe thermally isolated from other stacks). Furthermore, only one stackmay be used instead of a plurality of stacks.

In this embodiment, electrical energy is stored and released in anenergy storage device, such as one or more capacitors and batteries. Theelectrical energy is stored in a storage device when the stack outputpower is above the average total desired or required output power. Thestored electrical energy is released from the storage device when theoutput power is below the average total desired or required outputpower.

Preferably, the system of this embodiment comprises a plurality of solidoxide fuel cell stacks. The output power of each of the plurality ofsolid oxide fuel cell stacks is periodically cycled above and below anaverage desired or required output power at the same time. In otherwords, all of the stacks in this embodiment are either at a high or lowoutput power at the same time. In this case, the combined thermaldissipation of the plurality of the stacks is still higher compared tothe thermal dissipation of the plurality of the stacks operated at aconstant output power over the period of time.

In the third embodiment, the same power controller/power conditioningsystem may be used to operate all of the stacks. Furthermore, the sameamount of fuel may be supplied to all of the stacks in the system. Thus,the system design is simplified since only one power controller/powerconditioning system and one fuel supply control device is needed for thewhole system. Preferably, the fuel supply control device controls thesupply of fuel to provide a lower amount of fuel to the stacks duringlow output power part of the cycle than during a high output power partof the cycle. Likewise, if desired, an oxidizer supply control device,such as an air blower or valve, controls the supply of oxidizer, such asair, to provide a lower amount of oxidizer to the stacks during lowoutput power part of the cycle than during a high output power part ofthe cycle.

The output power cycle frequency may range from high to low cyclefrequency. For example, the cycle frequency may range from severaloutput power variations per second, such as 2-20 variations per second,to one output power variation per one or more seconds, such as onevariation per 1-60 seconds, to one output power variation per one ormore minutes, such as one variation per 1-120 minutes, for example, onevariation per 1 to 10 minutes. Thus, each high and low output powerduration may last less than a second, several seconds, several minutesor even one or more hours.

SOFC stacks generally have significant thermal inertia and the operatingtemperature can in certain cases be allowed to drift slightly up ordown, such as by a few degrees, such as 5-20 degrees C., up to 100 C upor down. If one or more stacks are cycled between low and high load tomatch an average load the stack, then thermal dissipation will increase.It should be noted that the output power cycling is preferably not donein response to a different output power demand by the power consumer(i.e., a stand alone device or the power grid) which receives power fromthe fuel cell system. Thus, to increase the thermal dissipation, thefuel cell system output power is intentionally cycled above and belowthe output power (i.e., the average power) actually desired or requiredby the power consumer. The energy storage device is used to provide asubstantially constant output power to the power consumer such that theconsumer does not notice the output power cycling by the fuel cellsystem. Thus, the power consumer can receive power from both the fuelcell system and the energy storage device.

FIG. 3A illustrates a fuel cell system 1 according to a first preferredembodiment of the invention in which separate fuel inlet conduits andfuel controllers are used for different fuel cells. Preferably, thesystem 1 is a high temperature fuel cell stack system, such as a solidoxide fuel cell (SOFC) system or a molten carbonate fuel cell system.The system 1 may be a regenerative system, such as a solid oxideregenerative fuel cell (SORFC) system which operates in both fuel cell(i.e., discharge) and electrolysis (i.e., charge) modes or it may be anon-regenerative system which only operates in the fuel cell mode.

The system 1 contains a plurality of high temperature fuel cell stacks3. Each of the stacks 3 may contain a plurality of SOFCs, SORFCs ormolten carbonate fuel cells. Each fuel cell contains an electrolyte, ananode electrode on one side of the electrolyte in an anode chamber, acathode electrode on the other side of the electrolyte in a cathodechamber, as well as other components, such as separatorplates/electrical contacts, seals, fuel cell housing and insulation. Ina SOFC operating in the fuel cell mode, the oxidizer, such as air oroxygen gas, enters the cathode chamber, while the fuel, such as hydrogenand/or hydrocarbon fuel, enters the anode chamber. Any suitable fuelcell designs and component materials may be used.

The system 1 also preferably contains a plurality of reformers 9 andcombustors 15. However, for some systems, the reformers and/orcombustors may be omitted. For example, for systems that operatedirectly on hydrogen fuel, the reformers and combustors may be omitted.Each reformer 9 is adapted to reform a hydrocarbon fuel to a hydrogencontaining reaction product and to provide the reaction product to afuel cell stack 3. Each combustor 15 is preferably thermally integratedwith one or more of the plurality of the reformers 9 to provide heat tothe reformers 9. The term “thermally integrated” in this context meansthat the heat from the reaction in the combustor 15 drives the netendothermic fuel reformation in one or more reformers 9.

Humidified fuel is provided in each reformer through a respective fuelinlet conduit 23. The system 1 also contains one or more control devices24 adapted to independently control an amount of fuel being provided toeach reformer 9 through each fuel inlet conduit 23 in response to theload on each associate stack 3.

The one or more control devices 24 may comprise one or more flowcontrollers, such as fuel flow control valves, that are adapted tocontrol fuel flow into each fuel inlet conduit. Preferably, each flowcontroller valve 24 is located in each of the plurality of the fuelinlet conduits 23. The valves 24 may be controlled manually by anoperator or automatically controlled by a control system, such as acomputer or another electronic control system. If desired, instead ofmultiple valves 24, a single, centrally located flow control device,such as a multi-outlet valve, may be used to independently control thefuel flow into each of the fuel inlet conduits 23 from one or more fuelsupply conduits 30 or fuel vessels.

Each reformer 9 is operatively connected to a respective stack 3 anodeinlet via a conduit 17 to provide a reformed product or fuel into eachstack 3. Air is provided into each stack 3 through a cathode inlet 19.The cathode exhaust outlet 10 of each fuel cell stack 3 is preferablyoperatively connected to an inlet 25 of at least one combustor 15 toprovide an oxidizer, such as hot air, into the combustor 15.

The term “operatively connected” means that components which areoperatively connected may be directly or indirectly connected to eachother. For example, two components may be directly connected to eachother by a fluid (i.e., gas and/or liquid) conduit. Alternatively, twocomponents may be indirectly connected to each other such that a fluidstream passes between the first component to the second componentthrough one or more additional components of the system.

Each of a plurality of hydrocarbon fuel sources or feed conduits 27 isalso operatively connected to a respective combustor 15 inlet 25.Preferably, each inlet 25 of each combustor 15 is connected to aseparate hydrocarbon fuel source or feed conduit 27. It should be notedthat for systems which lack the combustors and/or reformers, the fuelmay be provided directly into the fuel cell. The conduits 24 and 27 maybe connected to the same fuel supply conduit 30 or vessel, or theconduits 24, 27 may be connected to different fuel supply conduits orvessels. Thus, the same or different fuel may be provided to thereformers 9 and combustors 15, as desired.

The system 1 may also optionally contain one or more control devices 29adapted to independently control an amount of fuel being provided toeach combustor through each fuel feed conduit 27 to independentlycontrol a temperature of each combustor 15. The independent control of atemperature of each combustor 15 provides independent control of anamount of heat provided to each thermally integrated reformer 9, whichin turn provides an independent control of a temperature of eachthermally integrated reformer 9. Furthermore, the independent control ofa temperature of each reformer 9 provides independent control of atemperature of each associated stack 3 which receives the reactionproduct from the controlled reformer 9. In other words, by independentlycontrolling the fuel flow to the combustors 15, the temperature of eachassociated reformer 9 and stack 3 may also be independently controlled.The one or more control devices 29 may comprise one or more flowcontrollers, such as fuel flow control valves, that are adapted tocontrol fuel flow into each fuel feed conduit 27, similar to valves 24.One or more sensors may be located in the system 1 which are used todetermine if one or more reformers 9 require additional heat and/or howmuch additional heat is required. These sensors may be reformertemperature sensor(s) which measure the reformer temperature and/orprocess parameter sensor(s), which measure one or more of fuelutilization, stack efficiency, heat loss and stack failure/turndown. Theoutput of the sensor(s) is provided to a computer or other processorand/or is displayed to an operator to determine if and/or how muchadditional heat is required by each reformer. The processor or operatorthen independently controls each combustor's heat output based on thestep of determining to provide a desired amount heat from the controlledcombustor to the desired reformer.

The stacks 3 are electrically connected to a power system 51 comprisinga power conditioning and/or control subsystems via separate electricalconnections 53, such as via separate wires. The system 51 may compriseany suitable power conditioning subsystem which conditions electricalpower received from the fuel cell stacks. Preferably, the system 51 alsocomprises an electrical controller or controllers which control the loadon the stacks 3 and the power output generated by the stacks 3. Thepower conditioning and control functions may be provided by separatecomponents. Furthermore, the system 51 may comprise separate powerconditioning and/or control subsystems for each stack 3.

The hydrocarbon fuel reformers 9 may be any suitable devices which arecapable of partially or wholly reforming a hydrocarbon fuel to form acarbon containing and free hydrogen containing fuel. For example, eachfuel reformer 9 may be any suitable device which can reform ahydrocarbon gas into a gas mixture of free hydrogen and a carboncontaining gas. For example, the fuel reformer 9 may reform a humidifiedbiogas, such as natural gas, to form free hydrogen, carbon monoxide,carbon dioxide, water vapor and optionally a residual amount ofunreformed biogas by a steam methane reformation (SMR) reaction. Thefree hydrogen and carbon monoxide are then provided into the fuel inletof one or more the fuel cell stacks 3 which are operatively connected toeach reformer.

Preferably, each fuel reformer 9 is thermally integrated with one ormore of the fuel cell stacks 3 to support the endothermic reaction inthe reformer 9 and to cool the stack or stacks 3. The term “thermallyintegrated” in this context means that the heat from the reaction in thefuel cell stack 3 drives the net endothermic fuel reformation in thefuel reformer 9. The fuel reformer 9 may be thermally integrated withone or more fuel cell stacks 3 by placing the reformer and stack(s) inthe same hot box 31 and/or in thermal contact with each other, or byproviding a thermal conduit or thermally conductive material whichconnects the stack(s) to the reformer.

As shown in FIG. 3A, each reformer 9 is preferably located in closeproximity to at least one stack 3 to provide radiative and convectiveheat transfer from the stack 3 to the reformer. Preferably, the cathodeexhaust conduit of each stack 3 is in direct contact with a respectivereformer 9. For example, one or more walls of each reformer 9 maycomprise a wall of the stack cathode exhaust conduit 10 of the adjacentstack 3. Thus, each stack's cathode exhaust provides convective heattransfer from each stack 3 to one or more adjacent reformers 9.

Furthermore, if desired, the cathode exhaust from each stack 3 may bewrapped around the adjacent reformer 9 by proper ducting and fed to thecombustion zone of the combustor 15 adjacent to the reformer 9, as shownin FIGS. 4-6 and as described in more detail below.

The combustors 15 provide a supplemental heat to one or more reformers 9to carry out the steam-methane reformation (SMR) reaction during steadystate operation. Each combustor 15 may be any suitable burner which isthermally integrated with one or more reformers 9. Each combustor 15receives the hydrocarbon fuel, such as natural gas, and the stack 3cathode exhaust stream through inlet 25. However, if desired, anothersource of oxygen or air may be provided to the combustor 15 in additionto or instead of the stack cathode exhaust stream. For example, an airblower may be used to provide room temperature or preheated air into thecombustor 15 inlet 25. The fuel and the source of oxygen, such as thehot air from the cathode exhaust stream, are combusted in the combustorto generate heat for heating one or more reformers 9. The combustoroutlet may be operatively connected to a heat exchanger to heat one ormore incoming streams provided into the fuel cell stacks, if desired.

Preferably, the supplemental heat to each reformer 9 is provided from acombustor 15 which is operating during steady state operation of thereformer (and not just during start-up) and from the cathode (i.e., air)exhaust stream of the stack 3. When no heat is required by the reformer,the combustor unit acts as a heat exchanger. Thus, the same combustor 15may be used in both start-up and steady-state operation of the system 1.

Most preferably, the combustor 15 is in direct contact with one or morereformers 9, and the stack 3 cathode exhaust is configured such that thecathode exhaust stream contacts one or more reformers 9 and/or wrapsaround the reformer(s) 9 to facilitate additional heat transfer. Thislowers the combustion heat requirement for SMR. Preferably, eachreformer 9 is sandwiched between one combustor 15 and one or more stacks3 to assist heat transfer. However, if desired, a plurality ofcombustors 15 may be used to heat each reformer 9.

As shown in FIG. 3A, the system 1 preferably contains a plurality ofunits 200. Each unit 200 contains one stack 3, one reformer 9 and onecombustor 15. FIG. 3B illustrates a system 100 according to alternativeaspect of the present invention. The system 100 is similar to system 1,except that in the system 100, each unit 201/202 comprises more than onestack 3 and/or more than one reformer 9. Preferably, but notnecessarily, each unit 201/202 contains one combustor 15. A plurality ofunits 200 and 201/202 may be located in the same hot box 31 in order tooperate different stacks 3 at a different output power to transfer heatfrom stacks operating at a higher output power to the stacks operatingat a lower output power. However, if desired, each unit 201/202 may belocated in a separate hot box 31, with the two fuel cell stacks 3 ineach unit operating at a different output power. The details of eachunit 200, 201 and 202 will be described in more detail below withrespect to FIGS. 4, 5 and 6.

FIGS. 4-6 illustrate three exemplary configurations of one of aplurality of stack, reformer and combustor units of FIGS. 3A and 3B inthe hot box 31. However, other suitable configurations are possible. Thereformer 9 and combustor 15 shown in FIGS. 4-6 preferably comprisevessels, such as fluid conduits, that contain suitable catalysts for SMRreaction and combustion, respectively. The reformer 9 and combustor 15may have gas conduits packed with catalysts and/or the catalysts may becoated on the walls of the reformer 9 and/or the combustor 15.

The reformer 9 and combustor 15 unit can be of cylindrical type, asshown in FIG. 4A or plate type as shown in FIGS. 5A and 6A. The platetype unit provides more surface area for heat transfer while thecylindrical type unit is cheaper to manufacture.

Preferably, the reformer 9 and combustor 15 are integrated into the sameenclosure 31 and more preferably share at least one wall, as shown inFIGS. 4-6. Preferably, but not necessarily, the reformer 9 and combustor15 are thermally integrated with the stack(s) 3, and may be located inthe same enclosure or hot box 31, but comprise separate vessels from thestack(s) 3 (i.e., external reformer configuration).

FIGS. 4A and 4B show the cross-sectional top and front views,respectively, of one of a plurality of units 201 shown in FIG. 3B. Eachunit 201 contains two stacks 3, and a cylindrical reformer 9/combustor15 subunit 210. In a preferred configuration of the unit 201, fins 209are provided in the stack cathode exhaust conduit 10 and in thecombustor 15 combustion zone 207 to assist with convective heat transferto the reformer 9. In case where the reformer 9 shares one or more wallswith the cathode exhaust conduit 10 and/or with the combustion zone 207of the combustor 15, then the fins are provided on the external surfacesof the wall(s) of the reformer. In other words, in this case, thereformer 9 is provided with exterior fins 209 to assist convective heattransfer to the interior of the reformer 9. In addition to the cathodeexhaust conduit 10, each stack 3 contains an oxidizer (i.e., air) inletconduit 19, a fuel or anode inlet conduit 223 and a fuel or anodeexhaust conduit 225.

The combustion zone 207 of the combustor 15 is located in the core ofthe cylindrical reformer 9. In other words, the combustor 15 comprises acatalyst containing channel bounded by the inner wall 211 of thereformer 9. In this configuration, the combustion zone 207 is also thechannel for the cathode exhaust gas. The space 215 between the stacks 3and the outer wall 213 of the reformer 9 comprises the upper portion ofthe stack cathode exhaust conduit 10. Thus, the reformer inner wall 211is the outer wall of the combustor 15 and the reformer outer wall 213 isthe inner wall of the upper portion of stack cathode exhaust conduit 10.If desired, a cathode exhaust opening 217 can be located in theenclosure 31 to connect the upper portion 215 of conduit 10 with thelower portions of the conduit 10. The enclosure 31 may comprise anysuitable container and preferably comprises a thermally insulatingmaterial.

FIGS. 5A and 5B show the cross-sectional top and front views,respectively, of an alternative unit 202 containing two stacks 3 and aplate type reformer 9 coupled with a plate type combustor 15. In thisconfiguration, each combustor is thermally integrated with tworeformers. The configuration of the plate type reformer-combustorsubunit 220 is the same as the cylindrical reformer-combustor subunit210 shown in FIGS. 4A and 4B, except that the reformer-combustor subunit220 is sandwich shaped between the stacks. In other words, thecombustion zone 207 is a channel having a rectangular cross sectionalshape which is located between two reformer 9 portions. The reformer 9portions comprise channels having a rectangular cross sectional shape.The fins 209 are preferably located on inner 211 and outer 213 walls ofthe reformer 9 portions. The plate type reformer and combustion subunit220 provides more surface area for heat transfer compared to thecylindrical unit 210 and also provides a larger cross-sectional area forthe exhaust gas to pass through. Thus, in the embodiments of FIGS. 4 and5, each unit 201 and 202 contains two stacks 3, one combustor 15 and oneor two reformers 9, respectively.

FIGS. 6A and 6B show the cross-sectional top and front views,respectively, of one of a plurality of units 200 shown in FIG. 3A. Theunit 200 contains one stack 3 and a plate type reformer 9 coupled with aplate type combustor 15. In this configuration, each combustor isthermally integrated with one reformer. Exhaust gas is wrapped aroundthe reformer 9 from one side. One side of the combustion zone 207channel faces insulation of the container or hot box 31 or the stacks ofadjacent unit 200 while the other side faces the reformer 9 inner wall211. In this case, each unit 200 contains a single stack 3, reformer 9and combustor 15.

A method of operating the system 1 according to a first preferredembodiment of the present invention is described with reference to FIGS.3A and 3B. The power conditioning/control system 51 independentlycontrols the load on the stacks 3 and the output power of the stacks 3.

On the fuel side, the preheated hydrocarbon fuel inlet stream and steamenter each one of the reformers 9 through separately controlled inletconduits 23 where the fuel is reformed into a reformate (i.e., ahydrogen and carbon containing gas). The valves 24 control the amount offuel provided to each reformer 9 based on the load and output power ofeach stack 3 which receives the reformed fuel from each reformer 9. Thereformed fuel (i.e., reformate) then enters the stack 3 anode inlet fromthe reformer 9 through conduit 17. The stack anode exhaust stream existsthe anode outlet 225 of the stack 3 and may be provided to a heatexchanger where it preheats a stream being provided into one or morestacks 3.

A preheated air inlet stream is provided into the cathode inlet 19 ofeach of the stacks 3. The air then exits the stack 3 as a cathodeexhaust stream and wraps around one or more reformers 9. The cathodeexhaust stream then enters the combustion zone of the combustor 15through conduit 10 via opening 217 and inlet 25.

The system 1 is preferably configured such that the cathode exhaust(i.e., hot air) exits on the same side of the system as the inlet of thereformer 9. For example, as shown in FIG. 4B, since the mass flow of hotcathode exhaust is the maximum at the lower end of the device, itsupplies the maximum heat where it is needed, at feed point of thereformer 9 (i.e., the lower portion of the reformer shown in FIG. 4B).In other words, the mass flow of the hot air exiting the stack ismaximum adjacent to the lower portion of the reformer 9 where the mostheat is needed. However, the cathode exhaust and reformer inlet may beprovided in other locations.

Desulfurized natural gas or another hydrocarbon fuel is also suppliedfrom the fuel feed conduits 27 into the inlets 25 of the combustors 15.Natural gas is injected into the central combustion zone 207 of thecombustor 15 where it mixes with the hot cathode exhaust. The circularor spiral fins are preferably attached to the inner 211 and outer 213reformer walls to assist heat transfer. Heat is transferred to the outerwall 213 of the reformer 9 from the stack 3 by convection and radiation.Heat is transferred to the inner wall 211 of the reformer by convectionand/or conduction from the combustion zone 207. As noted above, thereformer and combustion catalysts can either be coated on the walls orpacked in respective flow channels. The exhaust stream from each of thecombustors 15 then preferably enters a heat exchanger where it exchangesheat with an incoming stream being provided to one or more stacks 3.

The foregoing description of the invention has been presented forpurposes of illustration and description. It is not intended to beexhaustive or to limit the invention to the precise form disclosed, andmodifications and variations are possible in light of the aboveteachings or may be acquired from practice of the invention. Thedescription was chosen in order to explain the principles of theinvention and its practical application. It is intended that the scopeof the invention be defined by the claims appended hereto, and theirequivalents.

What is claimed is:
 1. A method of operating a high temperature fuelcell system comprising fuel cell stacks divided into at least a firstgroup and a second group, each group including at least one of the fuelcell stacks, the method comprising: outputting substantially the sameoutput power from the first and second groups, such that the first andsecond groups collectively output a predetermined output power; andincreasing a power output of the first group to a first output power,and decreasing a power output of the second group to a second outputpower that is less than the first output power; wherein a sum of thefirst and second output powers is at least equal to the predeterminedoutput power.
 2. The method of claim 1, wherein a combined thermaldissipation of the fuel cell stacks, when the first group outputs thefirst power and the second group outputs the second power, is higherthan a combined thermal dissipation of the fuel cell stacks when thefirst and second groups output a same output power.
 3. The method ofclaim 2, wherein each one of the fuel cell stacks is thermallyintegrated with one or more other fuel cell stacks, such that each oneof the fuel cell stacks provides dissipated heat to one or more otherfuel cell stacks or absorbs heat from one or more other fuel cellstacks.
 4. The method of claim 1, further comprising separatelycontrolling an amount of fuel provided to each of the fuel cell stacks,such that more fuel is provided to the first group when outputting afirst output power than to the second group when outputting the secondoutput power.
 5. The method of claim 1, wherein each of the fuel cellstacks is separately electrically connected to at least one of a powerconditioning subsystem and a power control subsystem.
 6. The method ofclaim 1, wherein the fuel cell stacks comprise solid oxide fuel cellstacks, and further comprising operating three or more groups of fuelcell stacks at different output powers.
 7. The method of claim 1,wherein the first group and the second group each comprise at least twoof the fuel cell stacks.
 8. The method of claim 1, wherein the firstgroup and the second group each comprise the same number of fuel cellstacks.
 9. The method of claim 1, further comprising supplying fuel tothe fuel cell stacks using a common fuel supply.
 10. The method of claim1, wherein the predetermined output power is value a desired totaloutput power from the plurality of fuel cell stacks.